Protein Recovery

ABSTRACT

A process for recovering a protein-containing fermentation agent, comprising (i) forming an aqueous mixture of an organic material and a protein-containing fermentation agent capable of fermenting the organic material to produce ethanol, (ii) fermenting the aqueous mixture to produce ethanol, (iii) recovering from the fermented aqueous mixture an ethanol stream which is rich in ethanol and a co-product stream comprising unfermented organic material, fermentation agent and an aqueous solution of dissolved solids in water, (iv) subjecting the co-product stream to a first separation stage to recover a first stream rich in the unfermented organic material and a second stream rich in the fermentation agent suspended in the aqueous solution, and (v) subjecting the second stream to a second separation step, capable of recovering suspended solids from a liquid, to recover a third stream rich in the fermentation agent and a fourth stream rich in the aqueous solution. The invention also relates to a new yeast composition obtainable from the process.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a continuation of and claims priority to U.S. patentapplication Ser. No. 13/257,895 filed Jan. 6, 2012 entitled “ProteinRecovery” which is a filing under 35 U.S.C. 371 of InternationalApplication No. PCT/GB2010/000577 filed Mar. 25, 2010 entitled “ProteinRecovery,” claiming priority of Great Britain Patent Application No.0905234.1 filed Mar. 26, 2009, which applications are incorporated byreference herein in their entirety.

FIELD OF INVENTION

The present invention relates to recovery of protein-containingmaterial, and more particularly relates to a process for recovering aprotein-containing material, such as yeast, from a bio ethanol process.The invention also relates to a new protein-containing composition,which may be obtained as a co-product of a bio ethanol process. Theprotein-containing composition according to the invention isparticularly useful in animal feed material.

BACKGROUND OF INVENTION

It has been known for many years to use bio ethanol refineries toconvert biological material into useful chemical products. In a typicalbio refinery, a plant material, such as grain containing starch (e.g.,wheat or maize), is treated to produce ethanol (so-called “bioethanol”). The process can be used to produce both potable alcohol andindustrial ethanol.

For example, in a conventional bio ethanol plant, wheat is fermentedusing yeast as the fermentation organism to produce bio ethanol as amain product and by-products, such as animal feed. The ratio of bioethanol to by-products is approximately 1:1, on a weight basis.

The principle by-product of a bio ethanol plant is called distillersdark grains and solubles (“DDGS”). DDGS is used in the animal feedmarket, primarily as a feedstock for ruminants. In a conventionalprocess, after the ethanol has been produced by fermentation, it isseparated from the fermentation products by distillation.

The residue after distillation of the ethanol (termed whole stillage) isthen dried to produce the by-product, DDGS. To aid in drying, the wholestillage is separated into two fractions, a solids fraction and a liquidfraction. This first separation may be carried out in a decanter toproduce a solid and a liquid output. The solid output may be pressedinto a cake. The liquid output is subjected to evaporation to make asyrup containing, among other things, yeast—this syrup is known ascondensed distiller's solubles (CDS). The CDS is then added to thepressed cake and dried to form what is known as the DDGS.

Although the bio ethanol process has been used for many years, verylittle work has been done on further development of the by-products ofthe process, and there is very little published information aboutby-product development.

In a paper by J. Knott and G. Shurson (Effects of feeding dietscontaining spray dried corn condensed distiller's solubles (CDS) andassociated fractions on growth performance of early-weaned pigs), J.Knott, G. Shurson, M. Hathaway, and L. Johnston, J. Anim Sci. Vol 83(Supp1.2) p. 71; Ethanol Byproduct may be a diet alternative, NationalHog Farmer. Feb. 15, 2005) work was done on the CDS by-product of bioethanol plants. The authors separated the CDS into two products, yeastcream (YC) and residual solubles (RS). The products were tested forutility as feed additives in animal feed. The purpose of the study wasspecifically to test whether the by-products of the bio ethanol processhad any utility as growth factors.

The Knott/Shurson paper describes subjecting the CDS to a spray dryingprocess to separate the CDS into three fractions, called “sprayed drieddistiller's solubles,” “spray dried yeast cream,” and “spray driedresidual solubles.” This process would not be suitable for the largescale recovery of yeast, because its cost would be prohibitive.Furthermore, based on the disclosure of the Knott/Shurson paper, therewould be no motivation for the skilled person to seek to recover yeaston a large scale, as the paper is concerned with the use of smallquantities of yeast as a growth factor present in the mixture, and doesnot make any reference to the amount of yeast which may be available forrecovery from the CDS or the large scale recovery of yeast per se.

SUMMARY OF THE INVENTION

It is known that yeast is a by-product of the bio ethanol process, andindeed this is inevitable, as the process itself relies on the presenceof yeast for the fermentation.

Yeast has been used in the animal feed market for many years, when as adead yeast as feed material and live yeast as a feed additive. Yeast hasa high content of digestible protein, and is therefore potentiallyuseful as a feed material for use in animal feed. However, to date,yeast has not been used to any significant extent as a feed material,owing to the lack of availability of sufficient quantities of thematerial at a cost effective price compared to other feed materials. Incommercially available animal feeds, there is a wide range of highprotein feed materials of which, rape meal, soya bean meal, and fishmealare primary examples. There are some examples of dried yeast being usedon a commercial basis as a feed material for fish, but it has not beenused for animals, such as ruminants (cattle and sheep) or mono-gastrics,such as pigs. Yeast is mostly used as a feed additive in amountsgenerally less than 2 wt % of the total weight of animal feed when it isused with relevant claims to improve the performance of animals.

It would be desirable to use yeast as a feed material for supplyingdigestible protein to animals, but except in certain limitedcircumstances (such as the aquatic use mentioned above), it is notfeasible to do so. This is because of the cost of the available yeast istoo high.

During the bio ethanol fermentation process, the yeast is added into themixture after saccharification in order to ferment the carbohydratesubstrate. The quantity of yeast added may be large and sufficient toferment the substrate available or may be added in a smaller quantityand allowed to multiply in the medium to the point at which there issufficient yeast to ferment the total available carbohydrate.

We have now unexpectedly found that the quantity of yeast produced as aby-product of the bio ethanol production process is much higher than hadbeen appreciated. In particular, we have found that the amount of yeastproduced as a by-product is in the range 10-20 wt %, based on the totalweight of the by-products. This typically represents about 4-7 wt % ofthe total output mass from the process, which is much higher than theamount which would be expected.

We have also found that a new yeast containing composition can berecovered from a bio ethanol process, which has an unexpected positiveeffect on the growth of animals.

BRIEF DESCRIPTION OF THE DRAWINGS

Reference is now made to the accompanying drawings, in which:

FIG. 1 is a schematic drawing of an embodiment of a bio ethanol processaccording to the prior art.

FIG. 2 is a schematic drawing of an embodiment of a process forrecovering fermentation agent, in particular yeast, according to theinvention.

FIG. 3 is a more detailed drawing of part of the process shown in FIG.1.

DETAILED DESCRIPTION OF THE INVENTION

Ethanol had been produced from bio ethanol plants on a large scale forthe past 15 to 20 years. For example, the European annual capacity forbio ethanol production in 2008 had risen to over 4 billion litres.However, in the prior art, the yeast fraction has never been recoveredon a commercial scale either from the process itself or from by-productsof the bio ethanol process, because it had not been appreciated thatthere was a significant amount of it present, or that it could beefficiently recovered. In the prior art, the yeast was not available ata price or quantity such that it could be conveniently used as a feedmaterial in animal feed.

According to one aspect of the invention, there is provided a processfor recovering a protein-containing fermentation agent, comprising:forming an aqueous mixture of an organic material and aprotein-containing fermentation agent capable of fermenting the organicmaterial to produce ethanol; fermenting the aqueous mixture to produceethanol; recovering from the fermented aqueous mixture an ethanol streamwhich is rich in ethanol and a co-product stream comprising unfermentedorganic material, the fermentation agent and an aqueous solution ofdissolved solids in water; subjecting the co-product stream to a firstseparation stage to recover a first stream rich in the unfermentedorganic material and a second stream rich in the fermentation agent,which is suspended in the aqueous solution; subjecting the second streamto a second separation step, capable of recovering suspended solids froma liquid, to recover a third stream rich in the fermentation agent and afourth stream rich in the aqueous solution; and, if necessary, dryingthe third stream to recover a composition comprising the fermentationagent.

The fermentation agent may be any agent used in the fermentation oforganic materials to produce ethanol. In one embodiment, thefermentation agent comprises, and more preferably consists of, fungalcells. More specifically, the fungal cells comprise, and more preferablyconsist of, single-celled ascomycetous fungal cells, particularly yeast.In the preferred embodiment, the yeast is of the genus Saccharomyces.Yeast of the genus Saccharomyces Carlsbergiensis is particularlysuitable.

In the following description, the process will be described withparticular reference to the recovery of yeast, but it will beappreciated that this description is equally applicable to the recoveryof protein containing fermentation agents, including microbialprotein-containing cells other than yeast. Furthermore, in anotherembodiment, the fermentation agent may be a bacterial fermentationagent, such as zymomonas mobilis. The process according to the inventionis suitable for any process for the fermentation of organic material toform ethanol (which may be ethanol for industrial use, or potableethanol). In general, by “fermentation” is meant the biological processby which sugars, such as glucose, fructose and sucrose are converted tocarbon dioxide and ethanol.

In accordance with conventional processes, the ethanol stream may beseparated from the co-product stream by distillation.

It has not previously been appreciated that the yeast is present in theco-product stream as a suspension, and that it may be separated from theco-product stream by any process suitable for removing a solidsuspension from a liquid. In an advantageous embodiment, the separationprocess is a mechanical separation process, in particularcentrifugation. One particularly advantageous process for separating theyeast from the other co-products is known as disk stack separation whichemploys centrifugal force to separate particulate matter from a liquid.The technique of disk stack separation, per se, is known in the art, butit has not previously been applied to the process according to theinvention.

The co-product stream is known in the art as “whole stillage.” Itcomprises predominantly water, undissolved unfermented organic materialand undissolved fermentation agent, such as yeast. It also containsnon-starch polysaccharides. For example, when the fermented organicmaterial is wheat, the whole stillage contains NSPs based on arabinose,urinic acid, glucan, xylose, and glucose residues and also containsglucomannan. The NSPs in wheat are approximately 25 wt % water solubleand 75 wt % water insoluble. Of the soluble fraction over 90 wt % of theNSPs are arabinoxylan or beta-glucan, with the remainder beinggalactose. The water is an aqueous solution containing dissolved solids,including unfermented soluble organic material. According to theinvention, the undissolved unfermented organic material, which istypically of a fibrous consistency, is separated from the rest of thewhole stillage in a first separation step, leaving the aqueous solutionand the fermentation agent. It will be appreciated that the unfermentedorganic material separated from the rest of the whole stillage willstill contain some fermentation agent and some of the aqueous solution.However, the majority of the fermentation agent and the aqueous solutionis separated from the undissolved unfermented material in the firststage of the separation. The undissolved unfermented organic materialmay contain a useful amount of the fermentation agent, such as yeast.Therefore, if desired, part of the recovered undissolved unfermentedorganic material may be recycled back into the co-product stream toimprove the yield of fermentation agent.

It has not previously been recognised that the fermentation agent, inparticular the yeast, is suspended in the aqueous solution and can bereadily separation by a mechanical separation technique, or equivalent.Thus, the majority of the fermentation agent, in particular the yeast,may be separated from the aqueous solution. However, the recoveredfermentation agent, in particular the yeast, does usually include someof the aqueous solution (including dissolved solids such as solublenon-starch polysaccharides), and therefore it is preferably dried afterrecovery.

In a preferred embodiment, the third stream is subjected to a dewateringstep. The dewatering step preferably comprises a mechanical dewateringstep. The mechanical dewatering step preferably comprises subjecting thethird stream to a filter press. It is preferred that the third stream isfurther dried, preferably by evaporation, preferably with heating, afterthe dewatering step.

It is particularly advantageous that the fermentation agent, inparticular the yeast, is separated from the stillage prior to subjectingthe stillage or fermentation agent to any drying or evaporation step.However, it is possible, to dry the stillage, including the yeast, priorto any separation step, then to wet it again, by adding water, when itis desired to separate the fermentation agent from the stillage. Thismay be useful, for example, when it is desired to separate thefermentation agent from the stillage at a different location from thebio refinery.

The fibrous co-product (i.e., the separated undissolved unfermentedorganic material) may be processed into a cake to form Distillers Driedgrains (DDG).

According to another aspect of the invention, there is providedapparatus for producing ethanol and a fermentation agent, comprising: afermentation stage for fermenting an aqueous mixture comprising anorganic material and a protein-containing fermentation agent capable offermenting the organic material, to produce ethanol; a first separationstage for recovering the ethanol from the unfermented aqueous mixture; asecond separation stage, downstream of the first separation stage forrecovering unfermented organic material from the fermentation agent andan aqueous solution of dissolved solids in water; and a third separationstage, downstream of the second separation stage, for separating thefermentation agent into a third stream rich in the fermentation agentand a fourth stream rich in the aqueous solution. Optionally, a drier isprovided for drying the third stream.

The starting material for the process may be any organic material (inparticular, a starch-containing material or a cellulose-containingmaterial) capable of being fermented with the fermentation agent toproduce ethanol. Thus, the starting material may be a cereal grain, suchas maize, wheat, sorghum, or barley, or may be potato or beet.Alternatively, the organic material may be straw, wood, or corn stover.The ethanol output may be of a grade used for industrial or fuel use, orit may be of a grade used for human consumption, such as a variety ofwhisky.

It will be appreciated that the fermentation agent may, and usuallywill, alter in nature during the course of the process. In general, thefermentation agent used in the fermentation step is “unspent,” wherebyit is capable of fermenting the organic material. The fermentation agentin the co-product stream may be a mixture of spent and unspentfermentation agent, and is usually substantially entirely spentfermentation agent.

Thus, when the fermentation agent is yeast, unspent (or “live”) yeastwill be employed during the fermentation process, and by the end of theprocess, when recovered in the co -product stream, some or all of theyeast will be spent (or “dead”) yeast.

In this specification, the expression “fermentation agent” may refer tounspent or spent fermentation agent, and the expression “yeast” mayrefer to unspent or spent yeast. The composition will be clear to aperson skilled in the art from the context in which the terms are used.

According to another aspect of the invention, there is provided aprocess for treating stillage, the stillage being obtained from afermentation process, especially an ethanol fermentation process, andcomprising water, yeast, suspended fibrous and non-fibrous solids anddissolved solids, the process comprising: separating the majority of thesuspending fibrous solids from the rest of the stillage; and thenseparating the majority of the yeast from the water and dissolvedsolids. It will be appreciated that the process according to the aspectof the invention may be provided with any desired combination of thefeatures described above in relation to the first aspect of theinvention.

The recovered fermentation agent, especially the yeast (typical examplesSaccharomyces cerevisiae; Saccharomyces Carlsbergiensis) produced by theprocess or apparatus according to the invention may be formulated forany desired end use, and may be formulated for use as a micronutrientfeed additive. However, it is particularly preferred that thefermentation agent, especially the yeast, produced by the processaccording to the invention is formulated as a feed material in an animalfeed composition. The fermentation agent, especially the yeast, may beas a feed material for ruminant animals, such as cattle, sheep andgoats. It is particularly preferred that the feed material containingthe fermentation agent, especially the yeast, is formulated to feedmonogastric animals, such as pigs, poultry, fish, crustacea andcompanion animals, such as horses, cats and dogs.

The main components of the organic dry matter of food are defined ascarbohydrates, lipids, proteins, nucleic acids, organic acids andvitamins (Animal Nutrition, third edition, P. McDonald, R.A. Edwards andJ. F. D. Greenhalgh, ISBN 0-582-44399-7). Typically, the fermentationagent, especially the yeast, would be formulated in an animal feedcomposition in the range from 2 to 40 wt %, preferably 3 to 40 wt %,more preferably 4 to 40 wt %, still more preferably 5 to 40 wt %, withthe remainder comprising those components as defined above. In addition,the food may contain a wide range of additives which according to thedefinition are feed materials which have some special effect, e.g.,provide enhanced performance. The protein in the feed material may beprovided partly or entirely by the fermentation agent, especially theyeast, produced by the process or apparatus according to the invention.

Other ingredients, such as selected amino acids (such as lysine,methionine, and so on), and vitamins (such as A, D, E, and so on),minerals (such as calcium, phosphorus, and so on) and antibiotics mayalso be present in the composition.

The process and apparatus according to the present invention produce ahigh value protein-containing composition as a co-product, rather thanthe relatively low value DDGS by-product produced in the prior art. Theprotein-containing composition can be produced on a scale large enoughto enable it to be used as a feed material in animal feed.

As mentioned above, the process and apparatus according to the inventionhave led to a new composition that has not been described in the artbefore.

Thus, according to another aspect of the invention, there is provided aprotein containing composition obtainable by a process as describedabove.

Furthermore, according to a still further aspect of the invention, thereis provided a protein-containing composition comprising yeast incombination with at least one, and preferably more than one, non-starchpolysaccharide (NSP), wherein the yeast comprises at least 60 wt % ofthe composition, based on the dry weight of the composition. Preferably,the composition comprises at least 65 wt % yeast, based on the dryweight of the composition. More preferably, the composition comprises atleast 75 wt % yeast, based on the dry weight of the composition. Stillmore preferably, the composition comprises at least 90 wt % yeast, basedon the dry weight of the composition. Most preferably, the compositioncomprises at least 90 wt % yeast, based on the dry weight of thecomposition. In these embodiments, the composition typically contains atmost 99.5 wt % yeast, 99 wt % yeast, 98 wt % yeast or 95 wt % yeast,based on the dry weight of the composition. The most preferredcompositions have from 60 to 95 wt % yeast, based on the dry weight ofthe composition, most preferably 90 to 95 wt % yeast, based on the dryweight of the composition.

Preferably, the yeast also includes sucrose; at least one reducingsugar; at least one mineral; at least one water soluble oligosaccharide;or a combination thereof. The reducing sugar may be glucose, fructose,lactose, or a combination thereof. Preferably, the composition contains0 to 8 wt % reducing sugar, more preferably 2 to 8 wt % reducing sugar,still more preferably 4 to 8 wt % reducing sugar and most preferablyabout 6 wt % reducing sugar.

Preferably, the composition contains 0 to 10 wt % sucrose, morepreferably 4 to 10 wt % sucrose, most preferable about 8 wt % sucrose.

Preferably, the composition contains 0 to 4 wt % mineral, mostpreferably about 2 wt % mineral. The mineral content may containcalcium, magnesium, phosphorous, potassium, sodium, copper, manganese,zinc, or a combination thereof.

The or each NSP is preferably present in an amount up to 10 wt % of thecomposition. More preferably the NSP is present from 0.1 to 10 wt %,more preferably from 0.1 to 5 wt % more preferably from 1-3 wt % andmost preferably about 2 wt %. Preferably, the NSP comprisesarabinoxylan, beta-glucan, galactose, or a combination thereof. In anembodiment, the NSP comprises arabinoxylan and beta-glucan. In anotherembodiment, the NSP comprises beta-glucan and galactose. In anotherembodiment, the NSP comprises arabinoxylan and galactose. In anotherembodiment, the NSP consists of arabinoxylan, beta-glucan, andgalactose. In another embodiment, the NSP comprises arabinoxylan,beta-glucan, and galactose. Preferably, the NSP comprises at least 90 wt% arabinoxylam and beta-glucan, and more preferably the balance isgalactose.

The water content of the composition is preferably 5 to 10 wt %,typically 8 wt %.

It will be apparent that the protein-containing composition according tothe invention may be readily produced by the process and apparatusaccording to the invention, as discussed above. However, this is a newproduct, which may also be produced by other means, such as by mixingyeast from another source with a preselected amount of NSPs.

According to another aspect of the invention there is provided a feedmaterial comprising a protein-containing composition as described above.Typically, the feed material comprises 2 to 40 wt %, of theprotein-containing composition according to the invention, preferably 3to 40 wt %, more preferably 4 to 40 wt %, still more preferably 5 to 40wt %. The remainder of the composition may be made up with other desiredcomponents, such as a carbohydrate source, and/or a lipid source, and/orfood additives. We have surprisingly found that the compositionsproduced by the above described process and the composition according tothe invention is useful in stimulating growth of animals. In particular,the compositions are useful in the non-therapeutic stimulation of growthin animals.

Thus, according to another aspect of the invention, there is provided amethod of stimulating growth in an animal comprising administering agrowth stimulating amount of a composition as described above.

The method is particularly useful in stimulating growth in cattle,sheep, goats, pigs, poultry, fish, crustacea, horses, cats, and dogs.

The protein composition according to the invention may be included indietary formulations for livestock as an alternative source of proteinto replace a range of protein materials that are currently used eitherindividually or in a mixture in feed (e.g., fishmeal; soya bean meal;rapeseed meal; maize gluten meal; pea protein). As such, the proteincomposition could replace from 0.5% to 100% of the individual proteinsor mixture of proteins in the diet. Preferably, the protein compositionaccording to the invention may replace about 5 to 40 wt % of theproteins in the proteins in the diet, more preferably about 20 to 35 wt%. Typically, the protein composition according to the invention mayreplace about 30 wt % of the proteins in the diet—this is especiallyappropriate for fish.

Over a wide range of species (pigs, poultry, fish) the intake per unitmetabolic weight (W0.75) of the protein composition according to theinvention may range from 0.01 to 90 g dry matter/W0.75/day.

With reference to FIG. 1, a source of fermentable carbohydrate, moreparticularly a source of starch, such as wheat or maize, is fed to amilling stage 10, then slurried with water to form a mash in a mashingstage 12. The first step in starch breakdown involves saccharification,typically using {acute over (α)}-amylase and steam. This is followed bya liquefaction stage 14, using steam from a stage 16. Further, enzymes(e.g., gluco amylase) are added in a saccharification stage 18, andyeast is added in fermentation stage 20.

The fermentation produces ethanol and co-products which are dischargedto a distillation stage 22, in which the majority of the ethanol isseparated by distillation from the majority of the co-products. Oneoutput from the distillation stage 22 is an ethanol rich stream, whichis fed to a rectification stage 24, in which the ethanol is furtherpurified. Steam from stage 16 is also fed to the rectification stage 24.

The purified ethanol from the rectification stage 24 is fed to adehydration stage 26, to which further steam from the stage 16 is added.The output from the dehydration stage 26 is discharged to an ethanolstorage stage 28.

The co-products from the distillation stage 22, known as whole stillage,are fed to a spent wash tank stage 30, and subsequently to a decanter32, which separates the solid unfermented organic material from anaqueous phase comprising mostly water and yeast.

The solids output 34 from the decanter 46 is pressed into a cake in acompression stage 36. The liquid output 32 from the decanter 46 is fedto an evaporation stage 38, which removes some water, followed by afurther heating stage 40, which removes more water to produce a syrup.This syrup typically has a moisture content of 75 wt % water. The syrupfrom stage 40 is sprayed onto the cake in a stage 56, and the resultantsprayed cake is fed to a drying stage 42. The output from the dryingstage 42 is DDGS, which is fed to a pelleting stage 44, which may alsoinclude a cooling stage.

The process shown in the drawings is known as a “dry-grind” process, andthis is the preferred process. An alternative process, known as a“wet-grind” process may be used instead, in which an amount of fibre isseparated from the starch source prior to fermentation.

Referring now to FIGS. 2 and 3, the process according to the inventionis shown. Many of the stages used in the process according to theinvention may be identical to the stages shown in FIG. 1, and like partshave been designated with like reference numerals.

The solids output from the decanter 46, is still pressed into a cake instage 36, then dried and pelletised in stage 42 and 44.

We have found that the liquid output from the decanter comprises a largequantity of yeast suspended in water, and that the yeast can berecovered from the water in a simple mechanical separator. Recovery ofyeast at this stage has not been previously contemplated. Thus, theliquid output is fed to a disk stack separator 50 which separates theyeast from the liquid. The yeast is produced in a stream 52, which isfed to a yeast drier 54. The water is produced in a stream 48, which isfed to evaporators 56 to produce a syrup. This syrup may be sprayed ontothe DDGS cake, as described with respect to FIG. 1.

EXAMPLES

Reference is now made to the following examples.

Example 1

300 carp fingerlings were fed one of five diets in which the proteincontaining composition (yeast protein concentrate) was used to replacealternative dietary protein sources over the growth phase of carp fromapproximately 10 to 50 g live weight. The protein containing compositionwas used to replace 7.7, 15, 20 and 50% of the dietary protein.

There were three tanks of fish per treatment (20 fish per tank), witheach tank representing the experimental unit. Weight gain data wasanalysed by Analysis of Variance with Tukeys applied post hoc.

Table 1 shows weight gain was increased in all fish given dietscontaining the protein containing composition compared with the control.Furthermore, this was significant at 14 and 19.7%.

TABLE 1 Yeast tested at 7.5, 15, 20 and 50% of total dietary proteinlevel Carp trial 1 Initial Final P value (relative Treatments weight (g)weight (g) to control) Control 12.15 39.22 — 6% unwashed yeast 12.2341.38 0.186 14% unwashed yeast 12.27 45.92 <0.001 19.7% unwashed yeast12.42 48.00 <0.001 46% unwashed yeast 12.38 41.73 0.104

In the second trial, two forms of the protein containing compositionwere compared. Two tanks per treatment were used, each containing 25carp fingerlings. The unwashed form in which the protein containingcomposition contained the yeast plus the non starch polysaccharides asin trial 1 and a second composition in which the protein containingcomposition was washed to produce a pure yeast product.

TABLE 2 Comparison of washed and unwashed yeast protein concentratesCarp trial 2 Initial Final P value (relative Treatments weight weight tocontrol) Control 15.26 55.52 — 30% Unwashed yeast 15.20 60.00 0.947 30%Washed yeast 15.14 54.40 1.000

There was a tendency for the fish fed the diet containing the proteincontaining composition plus the non starch polysaccharides (unwashedyeast) to have weight gains which were higher than both the controls andthe fish given the diet containing the washed pure yeast product.

These examples shows that weight gain of fingerling carp wassignificantly increased when the protein containing composition was usedto supply 15-30% of dietary protein for carp. A yeast containing productderived from bio-ethanol production appears to provide a viablealternative protein source for use in commercial diets for fish.

Example 2

140 male Ross 308 chicks were fed one of seven wheat/soya beanmeal-based mash diets from 0 to 14 days of age. The diets used contained0, 3, 6 or 9% of two fermented wheat co-products, one from a potablealcohol source (yeast A) and one from a bio ethanol source (yeastB—i.e., a protein containing composition according to the invention,including NSPs). A control comprising soyabean meal was also used.

Data were analysed using a 2 by 3 factorial design using Genstat version12 for windows to examine the effects of yeast source and rate ofdietary inclusion on viscosity of ileal digesta supernatant, body weightgain, feed intake and feed conversion ratio.

Table 1 shows weight gain was significantly increased in birds fed thebio ethanol-derived yeast source (yeast B), compared to the potablealcohol-derived yeast source (yeast A). Feed intake was alsosignificantly increased in the birds fed diet B but no significantlydifference in feed conversion ratio (FCR) was observed between the twoyeast sources.

This example shows that yeasts increased broiler weight gain at thelower inclusion levels. Yeast derived from bio-ethanol productionappears to provide a viable alternative protein source for use inbroiler starter diets.

Mean weight Mean feed gain intake Treatment (S.E.) (g) (S.E.) (g) FCRControl 240.0 380.7 1.59 3% Yeast A 286.5 417.2 1.46 6% Yeast A 223.5346.8 1.55 9% Yeast A 202.5 326.9 1.61 3% Yeast B 328.4 467.3 1.42 6%Yeast B 330.4 457.0 1.38 9% Yeast B 265.2 427.8 1.61 Variation Source Pvalue Yeast source 0.023 0.019 0.114 RoI (L) 0.623 0.711 0.043 Yeast*RoI 0.399 0.461 0.598

It will be appreciated that the invention described above may bemodified in accordance with the following claims.

1. A process for recovering a protein-containing fermentation agent,comprising: (i) forming an aqueous mixture of an organic material and aprotein-containing fermentation agent capable of fermenting the organicmaterial to produce ethanol; (ii) fermenting the aqueous mixture toproduce a fermented aqueous mixture comprising ethanol; (iii) recoveringfrom the fermented aqueous mixture an ethanol stream which is rich inethanol and a co-product stream comprising unfermented organic material,fermentation agent and dissolved solids in water; (iv) subjecting theco-product stream to a first separation stage to recover a first streamrich in the unfermented organic material and a second stream rich in thefermentation agent suspended in water; and (v) subjecting the secondstream to a second separation stage, capable of recovering suspendedsolids from a liquid, to recover a third stream rich in the fermentationagent and a fourth stream comprising dissolved solids, suspended solids,or both in water.
 2. The process according to claim 1, wherein the firstseparation stage comprises a mechanical separation stage.
 3. The processaccording to claim 2, wherein the mechanical separation stage includes adecanting stage.
 4. The process according to claim 1, wherein the firstseparation stage includes a centrifugal separation stage.
 5. The processaccording to claim 1, wherein the second separation stage comprises amechanical separation stage.
 6. The process according to claim 5,wherein the mechanical separation stage of the second separation stageincludes a centrifugal separation stage.
 7. The process according toclaim 6, wherein the centrifugal separation stage is carried out using adisk stack separator.
 8. The process according to claim 7, wherein thethird stream is subjected to a dewatering stage.
 9. The processaccording to claim 8, wherein the dewatering stage comprises amechanical dewatering stage.
 10. The process according to claim 9,wherein the mechanical dewatering stage comprises subjecting the thirdstream to a filter press.
 11. The process according to claim 8, furthercomprising drying the third stream, after the dewatering stage, tofurther reduce the moisture content.
 12. The process according to claim11, wherein the unfermented organic material is processed into a cakeafter separation from the co-product stream obtained from (i)-(iii) andwherein syrup is sprayed onto the cake, to produce distillers darkgrains and solubles (DDGS).
 13. The process according to claim 1,further comprising drying the third stream to reduce the moisturecontent.
 14. The process according to claim 1, wherein the fourth streamis subjected to an evaporation stage to produce a syrup.
 15. The processaccording to claim 1, wherein the organic material comprises afermentable carbohydrate.
 16. The process according to claim 1, whereinthe organic material comprises a cereal grain, maize, wheat, sorghum orbarley; potato; or beet molasses.
 17. The process according to claim 1,wherein the fermentation agent comprises fungal cells capable offermenting the organic material to ethanol.
 18. The process according toclaim 1, wherein the fermentation agent comprises a yeast.
 19. Theprocess according to claim 18, wherein the yeast is a yeast of the genusSaccharomyces.
 20. The process according to claim 1, further comprisingformulating the recovered fermentation agent as a feed additive in ananimal feed composition.
 21. The process according to claim 20, whereinthe fermentation agent comprises less than 2 wt % of the animal feedcomposition.
 22. The process according to claim 1, comprisingformulating the recovered fermentation agent as a protein source in afeed material in an animal feed composition.
 23. The process accordingto claim 22, wherein the fermentation agent comprises more than 2 wt %of the animal feed composition.
 24. The process according to claim 22,wherein the fermentation agent comprises more than 4 wt % of the animalfeed composition.
 25. The process according to claim 22, wherein thefermentation agent comprises from 5 wt % to 40 wt % of the animal feedcomposition.
 26. The process according to claim 22, further comprisingcombining the fermentation agent with a carbohydrate source, andoptionally an additional protein source, and optional additives, whereinthe fermentation agent comprises at least 2 wt % of the animal feedcomposition.
 27. The process according to claim 1, wherein theunfermented organic material is processed into a cake after separationfrom the co-product stream obtained from (i)-(iii).
 28. The processaccording to claim 27, wherein the co-product stream comprises water,protein-containing fermentation agent, suspended fibrous andproteinaceous non-fibrous solids and dissolved solids comprisingproteins.
 29. The process according to claim 28, further comprisingtreating the stillage by separating the majority of the suspendedfibrous solids from the rest of the co-product stream; and thenseparating the majority of the protein-containing fermentation agentfrom the water and dissolved solids.
 30. The process of claim 1, whereinproducing ethanol and a protein-containing fermentation agent accordingto (i)-(v) is carried out in an apparatus comprising: (i) a fermentationstage for fermenting an aqueous mixture comprising an organic materialand a fermentation agent capable of fermenting the organic material, toproduce ethanol; (ii) a first separation stage for recovering theethanol from the unfermented aqueous mixture; (iii) a second separationstage, downstream of the first separation stage for recoveringunfermented organic material from the fermentation agent and from anaqueous solution of dissolved solids in water; and (iv) a thirdseparation stage, downstream of the second separation stage, forrecovering the fermentation agent from the aqueous solution.